Patent Grant
9796591
Embodiments of the disclosure relate to the large-scale catalytic conversion of a carbon-containing feedstock into solid carbon, and, more specifically, to methods of converting mixtures of carbon monoxide, carbon dioxide, or any combination thereof to create carbon nanotube structures.
U.S. Patent Publication No. 2012/0034150 A1, published Feb. 9, 2012, the disclosure of which is hereby incorporated herein in its entirety by this reference, discloses background information hereto.
Additional information is disclosed in the following documents, the disclosure of each of which is hereby incorporated herein in its entirety by this reference:
1. International Patent Publication WO 2013/158159 A1, published Oct. 24, 2013, for “Methods and Systems for Thermal Energy Recovery from Production of Solid Carbon Materials by Reducing Carbon Oxides;”
2. International Patent Publication WO 2013/158160 A1, published Oct. 24, 2013, for “Methods for Producing Solid Carbon by Reducing Carbon Dioxide;”
3. International Patent Publication WO 2013/158157 A1, published Oct. 24, 2013, for “Methods and Reactors for Producing Solid Carbon Nanotubes, Solid Carbon Clusters, and Forests;”
4. International Patent Publication WO 2013/158158 A1, published Oct. 24, 2013, for “Methods for Treating an Offgas Containing Carbon Oxides;”
5. International Patent Publication WO 2013/158155 A1, published Oct. 24, 2013, for “Methods for Using Metal Catalysts in Carbon Oxide Catalytic Converters;”
6. International Patent Publication WO 2013/158161 A1, published Oct. 24, 2013, for “Methods and Systems for Capturing and Sequestering Carbon and for Reducing the Mass of Carbon Oxides in a Waste Gas Stream;”
7. International Patent Publication WO 2014/011206 A1, published Jan. 16, 2014, for “Methods and Systems for Forming Ammonia and Solid Carbon Products;” and
8. International Patent Publication WO 2013/162650 A1, published Oct. 31, 2013, for “Carbon Nanotubes Having a Bimodal Size Distribution.”
Solid carbon has numerous commercial applications. These applications include longstanding uses such as uses of carbon black and carbon fibers as a filler material in tires, inks, etc., many uses for various forms of graphite (e.g., pyrolytic graphite in heat shields) and innovative and emerging applications for buckminsterfullerene and carbon nanotubes. Conventional methods for the manufacture of various forms of solid carbon typically involve the pyrolysis of hydrocarbons in the presence of a suitable catalyst. Hydrocarbons are typically used as the carbon source due to historically abundant availability and relatively low cost. The use of carbon oxides as the carbon-source in the production of solid carbon has largely been unexploited.
Carbon oxides, particularly carbon dioxide, are abundant gases that may be extracted from point-source emissions such as the exhaust gases of hydrocarbon combustion or from some process offgases. Carbon dioxide may also be extracted from the air. Because point-source emissions have much higher concentrations of carbon dioxide than does air, they are often economical sources from which to harvest carbon dioxide. However, the immediate availability of air may provide cost offsets by eliminating transportation costs through local manufacturing of solid carbon products from carbon dioxide in air.
Carbon dioxide is increasingly available and inexpensive as a byproduct of power generation and chemical processes in which an object may be to reduce or eliminate the emission of carbon dioxide into the atmosphere by capture and subsequent sequestration of the carbon dioxide (e.g., by injection into a geological formation). For example, the capture and sequestration of carbon dioxide is the basis for some “green” coal-fired power stations. In current practice, capture and sequestration of the carbon dioxide entails significant cost.
There is a spectrum of reactions involving carbon, oxygen, and hydrogen wherein various equilibria have been identified. Hydrocarbon pyrolysis involves equilibria between hydrogen and carbon that favors solid carbon production, typically with little or no oxygen present. The Boudouard reaction, also called the “carbon monoxide disproportionation reaction,” is the range of equilibria between carbon and oxygen that favors solid carbon production, typically with little or no hydrogen present. The Bosch reaction is within a region of equilibria where all of carbon, oxygen, and hydrogen are present under reaction conditions that also favor solid carbon production.
The relationship between the hydrocarbon pyrolysis, Boudouard, and Bosch reactions may be understood in terms of a C—H—O equilibrium diagram, as shown in
CNTs are valuable because of their unique material properties, including strength, current-carrying capacity, and thermal and electrical conductivity. Current bulk use of CNTs includes use as an additive to resins in the manufacture of composites. Research and development on the applications of CNTs is very active with a wide variety of applications in use or under consideration. One obstacle to widespread use of CNTs has been the cost of manufacture.
U.S. Pat. No. 7,794,690 (Abatzoglou, et al.) teaches a dry reforming process for sequestration of carbon from an organic material. Abatzoglou discloses a process utilizing a 2D carbon sequestration catalyst with, optionally, a 3D dry reforming catalyst. For example, Abatzoglou discloses a two-stage process for dry reformation of an organic material (e.g., methane, ethanol) and CO2 over a 3D catalyst to form syngas, in a first stage, followed by carbon sequestration of syngas over a 2D carbon steel catalyst to form CNTs and carbon nanofilaments. The 2D catalyst may be an active metal (e.g., Ni, Rh, Ru, Cu—Ni, Sn—Ni) on a nonporous metallic or ceramic support, or an iron-based catalyst (e.g., steel), on a monolith support. The 3D catalyst may be of similar composition, or may be a composite catalyst (e.g., Ni/ZrO2—Al2O3) over a similar support. Abatzoglou teaches preactivation of a 2D catalyst by passing an inert gas stream over a surface of the catalyst at a temperature beyond its eutectic point, to transform the iron into its alpha phase. Abatzoglou teaches minimizing water in the two-stage process or introducing water in low concentrations (0 to 10 wt %) in a reactant gas mixture during the dry reformation first stage.
This disclosure relates generally to catalytic conversion processes for reducing carbon oxides to a valuable solid carbon product, and, in particular, to the use of carbon oxides (e.g., carbon monoxide (CO) and/or carbon dioxide (CO2)) as the primary carbon source for the production of solid carbon products (e.g., buckminsterfullerenes) utilizing a reducing agent (e.g., hydrogen or a hydrocarbon) in the presence of a non-ferrous catalyst. The methods may be used to manufacture solid carbon products in various morphologies and to catalytically convert carbon oxides into solid carbon and water. One of the morphologies that may be formed is single-wall carbon nanotubes.
In some embodiments, a method of reducing a gaseous carbon oxide to a lower oxidation state includes reacting a carbon oxide with a gaseous reducing agent in the presence of a non-ferrous metal catalyst in a non-oxidized state. The catalyst has a surface comprised of grains of a predetermined mean grain size. The reaction proceeds under predetermined conditions of temperature and pressure adapted to produce a solid carbon product.
In certain embodiments hereof, the partial pressure of water in the reaction is regulated by various means, including recycling and condensation of water, to influence, for example, the structure or other aspects of the composition of carbon products produced. The partial pressure of water appears to assist in obtaining certain desirable carbon allotropes.
In certain embodiments, a broad range of inexpensive and readily-available catalysts, including steel-based catalysts, are described, without the need for activation of the catalyst before it is used in a reaction. Iron alloys, including steel, may contain various allotropes of iron, including alpha-iron (austenite), gamma iron, and delta-iron. In some embodiments, reactions disclosed herein advantageously utilize an iron-based catalyst, wherein the iron is not in an alpha phase. In certain embodiments, a stainless steel containing iron primarily in the austenitic phase is used as a catalyst.
Catalysts, including an iron-based catalyst (e.g., steel, steel wool), may be used without a need for an additional solid support. In certain embodiments, reactions disclosed herein proceed without the need for a ceramic or metallic support for the catalyst. Omitting a solid support may simplify the setup of the reactor and reduce costs.
In other embodiments, a structure adapted to facilitate the reaction of a carbon oxide with a reducing agent includes a non-ferrous Bosch-type catalyst in a non-oxidized state configured to promote the reduction of the carbon oxide to a lower oxidation state. The non-ferrous Bosch-type catalyst includes a surface having a plurality of particles of catalyst material. The particles have a preselected mean grain size.
In certain embodiments, a method for utilizing a non-ferrous metallic compound in a reactor to reduce a gaseous carbon oxide includes purging gases in the reactor containing the non-ferrous metallic compound with a gaseous reducing agent and maintaining a predetermined reactor temperature sufficient to reduce oxides present in the metallic non-ferrous compound. A reaction gas mixture comprising the gaseous carbon oxide is introduced into the reactor to form a reaction gas composition at a reaction gas pressure. The reaction gas composition and reaction gas pressure are maintained in the reactor to reduce the gaseous carbon oxide.
Some methods of forming a solid carbon product include reacting a gaseous carbon oxide with a gaseous reducing agent in the presence of a catalyst comprising at least one of nickel, chromium, molybdenum, tungsten, cobalt, and alloys and mixtures thereof. The catalyst has a predetermined grain size selected to control the size and morphology of the solid carbon product.
Features and advantages of the disclosure will be apparent from reference to the following detailed description taken in conjunction with the accompanying drawings, in which:
The disclosure includes methods for reducing a carbon oxide to a lower oxidation state. The methods may be used to manufacture solid carbon products in various morphologies, and to convert carbon oxides into solid carbon and water. Solid carbon products may include graphite (e.g., pyrolytic graphite), graphene, carbon black, fibrous carbon, buckminsterfullerenes, single-wall CNTs, or multi-wall CNTs. The type, purity, and homogeneity of solid carbon products may be controlled by the reaction conditions (time, temperature, pressure, partial pressure of reactants, and/or catalyst properties).
The methods, based generally on the Bosch reaction, include reactions in the interior region of the phase diagram shown in
The methods use two abundant feedstocks: a carbon oxide (e.g., carbon dioxide, carbon monoxide, or a mixture thereof) and a reducing agent. The reducing agent may be a hydrocarbon gas (e.g., natural gas, methane, etc.), hydrogen gas (H2), another reducing gas, or a mixture thereof. A hydrocarbon gas may also be a source of additional carbon. Synthesis gas, referred to herein and in the art as “syngas,” includes primarily carbon monoxide and hydrogen, and syngas has both the carbon oxide and the reducing gas in a mixture. Syngas may be used as all or a portion of the reaction gas mixture.
The reduction processes described herein generally result in the formation of at least one solid carbon product and water. The water may subsequently be condensed. Latent heat of the water may be extracted for heating purposes or as part of a low-pressure power extraction cycle. The water may be a useful co-product used for another process.
The methods disclosed herein use carbon oxides (e.g., carbon dioxide) as an economically valuable feedstock. In many industrial processes, carbon dioxide is an undesirable waste product, and may have disposal costs (e.g., for sequestration). Use of carbon dioxide as an input for solid carbon production may reduce or eliminate disposal costs, and may simultaneously convert carbon oxides to a salable product. Thus, methods disclosed herein may be incorporated with fossil fuel combustion processes. This combination may be beneficial because the formation of solid carbon products by such processes may be more economical than conventional separation and sequestration methods.
Carbon dioxide is present in many natural gas deposits at various concentrations, such as at concentrations of up to 5% by volume, up to 20% by volume, up to 60% by volume, or even higher. Other compounds, such as H2S, SO2, and other sulfur compounds are often present in natural gas. Removal of sulfur-containing compounds is often done at a well site to form “sweet gas” (i.e., gas with little or no sulfur content). Removal of carbon dioxide before the natural gas is delivered to a consumer may be effectively accomplished via the techniques disclosed herein.
Solid carbon products such as buckminsterfullerene and carbon nanotubes may be formed by the catalytic conversion of carbon oxides to solid carbon and water. Carbon oxides may be derived from various sources, such as the atmosphere, combustion gases, process offgases, well gas, and other natural and industrial sources of carbon oxides. The carbon oxides may be separated from these sources and concentrated as needed, such as by amine absorption and regeneration.
The methods herein generally apply the Bosch reactions, such as the Bosch reaction of carbon dioxide with hydrogen to form solid carbon from carbon dioxide:
CO2+2H2C(s)+2H2O (Equation 1).
The type and quality of solid carbon produced may vary based on the type of catalysts, gas mixtures, and process variables (e.g., temperature, pressure, concentration of reactants and retention times). Solid carbon may be produced in many different morphologies through the carbon oxide reduction process disclosed herein. Some of the solid carbon morphologies that may be produced include graphite (e.g., pyrolytic graphite), graphene, carbon black, fibrous carbon, buckminsterfullerene, single-wall CNTs, multi-wall CNTs, platelets, or nanodiamond. The reactions occur in the interior region of the triangular equilibrium diagram shown in
The Bosch reactions use hydrogen or another reducing agent to reduce carbon oxides to solid carbon and water. The reactions may proceed in the presence of a non-ferrous catalyst at temperatures in excess of approximately 650° C., such as in excess of about 680° C. When the solid carbon is in the form of CNTs, Equation 1 is exothermic (heat producing) and releases approximately 24.9 kcal/mol at 650° C. (i.e., ΔH=−24.9 kcal/mol). Equation 1 is reversible, and solid carbon may be oxidized by water to form carbon dioxide. Although reaction temperatures above about 650° C. may be used to produce solid carbon nanotubes, if the temperature is too high, the rate of the reverse reaction of Equation 1 increases, and the net rate of reaction of carbon dioxide is lower. The equilibrium of Equation 1 generally shifts to the left as temperature increases.
The Bosch reactions are believed to be two-step reactions. In the first step of Equation 1, carbon dioxide reacts with hydrogen to create carbon monoxide and water:
CO2+H2CO+H2O (Equation 2).
Equation 2 is slightly endothermic at 650° C., requiring a heat input of about 8.47 kcal/mol (i.e., ΔH=+8.47 kcal/mol). In the second step of the reaction shown in Equation 1, carbon monoxide reacts with hydrogen to form solid carbon and water:
CO+H2C(s)+H2O (Equation 3).
Equation 3 may occur with stoichiometric amounts of reactants, or with excess CO2 or H2. Equation 3 is exothermic at 650° C., releasing 33.4 kcal/mol (1.16×104 joules/gram of C(s)) when CNTs are formed (i.e., ΔH=−33.4 kcal/mol). Values of ΔH for Equation 3 may be calculated for other carbon products by the difference between the ΔH value for Equation 1 for that particular carbon product and the ΔH value for Equation 2.
The Bosch reactions may be used to efficiently produce solid carbon products of various morphologies on an industrial scale, using carbon oxides as the primary carbon source. The Bosch reactions may proceed at temperatures from about 450° C. to over 2,000° C. The reaction rates typically increase in the presence of a catalyst.
A reducing gas mixture of one or more of the commonly available hydrocarbon gases such as lower hydrocarbon alkanes (e.g., methane, ethane, propane, butane, pentane, and hexane), including those found in natural gas, may be economical in some applications. In one embodiment, the reducing gas comprises methane and releases heat in an exothermic reaction in the presence of a non-ferrous catalyst and under reaction conditions optimized for the particular desired type of solid carbon:
CH4+CO22C(s)+2H2O (Equation 4).
Equation 4 is believed to be a two-step reaction, including the following steps:
CH4+CO22CO+2H2 (Equation 5); and
CO+H2C(s)+H2O (Equation 6).
In the presence of limited oxygen, hydrocarbons may react to form carbon monoxide, carbon dioxide, and water, as well as small hydrocarbons and hydrogen. Higher concentrations of oxygen may limit the amount of solid carbon formed. Therefore, it may be desirable to restrict the amount of oxygen present in reaction systems to optimize the production of solid carbon. Additionally, the presence of oxygen may poison catalysts, thereby reducing the reaction rates. Thus, the presence of oxygen may reduce the overall production of solid carbon products.
Carbon oxides used in the formation of solid carbon products may be the product of combustion of hydrocarbons, or may be from some other source. Carbon oxides may be injected with a reducing agent into a preheated reaction zone at a desired reaction temperature.
The reactions typically occur in the presence of a catalyst, which may be predominately composed of a non-ferrous metal. The catalyst composition, method of formation, catalyst grain size, and catalyst grain boundary conditions may influence the type, purity, and homogeneity of the solid carbon product. The reaction conditions, including the temperature and pressure of the reactor and the residence time of the reaction gases may be controlled to obtain solid carbon products having desired characteristics. The reactor feed gas mixture and reaction product are typically passed through the reactor and a condenser. The condenser may remove excess water and control the partial pressure of the water vapor in the reaction gas mixture.
The reaction kinetics favorable to the formation of the desired species of solid carbon may be established through the use of suitable catalysts. In certain embodiments, a carbon oxide is reduced in a reactor or catalytic converter containing a non-ferrous catalyst. As used herein, the term “non-ferrous catalyst” means and includes a catalyst including elements other than iron. Thus, a non-ferrous catalyst includes catalyst materials in which iron is present in combination with other elements or in which iron is not present. Typical catalysts include metals selected from groups 2 through 15 of the periodic table, such as from groups 5 through 10 (e.g., nickel, molybdenum, chromium, cobalt, tungsten, manganese, ruthenium, platinum, iridium, etc.), actinides, lanthanides, alloys thereof, and combinations thereof. Note that the periodic table may have various group numbering systems. As used herein, group 2 is the group including Be, group 3 is the group including Sc, group 4 is the group including Ti, group 5 is the group including V, group 6 is the group including Cr, group 7 is the group including Mn; group 8 is the group including Fe, group 9 is the group including Co, group 10 is the group including Ni, group 11 is the group including Cu, group 12 is the group including Zn, group 13 is the group including B, group 14 is the group including C, and group 15 is the group including N. For example, non-ferrous catalysts include nickel, cobalt, chromium, molybdenum, tungsten, and alloys thereof. Minor amounts of iron may be present in some alloys.
The non-ferrous catalyst may have a grain size proportional to the diameter of a desired carbon product. Non-ferrous catalysts may be in the form of nanoparticles or in the form of domains or grains and grain boundaries within a solid material. Non-ferrous catalysts may be selected to have a grain size related to a characteristic dimension of a desired diameter of the solid carbon product (e.g., a CNT diameter). In some embodiments, catalyst powder may be formed in or near the reaction zone by injecting a solution as an aerosol (i.e., a distribution of particles), such that upon evaporation of a carrier solvent, a selected particle size distribution results. Alternatively, powdered catalyst may be entrained in a carrier gas and delivered to the reactor. Entrainment may require the catalyst particles to be in relatively fine particles to effectively be transported by a carrier gas. By selecting the catalyst and the reaction conditions, the process may be tuned to produce selected morphologies of solid carbon product.
In the presence of a non-ferrous catalyst, reduction of carbon oxides typically proceeds to completion in under five seconds, and the reaction time can be as short as a few tenths of a second under the right process conditions and non-ferrous catalyst. Generally, shortening the reaction time or increasing the flow rate of the reactants through the reactor has the effect of decreasing the diameter of CNTs formed.
Non-ferrous catalysts may be provided on catalyst supports. A catalyst support can be any metal oxide or other material that can withstand the reaction conditions. For example, a support material may be selected to withstand elevated reaction temperatures in a reactor configured CNT synthesis. In some embodiments, catalyst support materials include Al2O3, SiO2, MgO, ZrO2, molecular sieve zeolites, and other oxidic supports. To control the properties of the solid carbon products formed on such catalysts, the metal loading on the catalyst support may be controlled, such as by leaving a portion of the surface of the support free of catalyst material. In some embodiments, catalyst materials may be provided without catalyst supports; thereby simplifying the preparation and reducing the cost of producing the solid carbon products.
For example, catalyst materials may be formed from catalyst precursors. Catalyst precursors may be mixed and dissolved in water or another solvent to make a solution of the catalyst precursors. The resulting solution may be dried to form the catalyst. In some embodiments, the solution may be sprayed to form an aerosol in a heated chamber, such as by atomization in a flow of gas, direct spraying of the solution through a nozzle, electrostatic spraying, dispersing the solution from the surface of a rotating fixture, and combinations thereof. In some embodiments, catalyst precursors may be combusted or otherwise decomposed by disposing a solution of catalyst precursor on a heated surface, allowing the solvent to evaporate, then allowing the catalyst precursor to combust. Other methods include creating the catalyst by a vacuum-deposition process at high vacuum (e.g., 10−6 to 10−8 Torr) and high temperatures (e.g., 900° C. to 1300° C.). Catalysts may be supplied as metal nanoparticles supported on solid supports via secondary dispersion and extraction. The catalyst may be mobilized, as in a fluidized bed, or may be stationary in the reactor as the carbon-containing gases flow through the reactor and react with the catalyst.
The catalyst particles may be nucleating sites from which CNTs grow. The catalyst particles may be domains or grains in a piece of metal material or discrete nanoparticles of catalytic metal deposited on an inert substrate (e.g., a quartz disk). The size of CNTs may be proportional to the size of the nucleating site. The ratio between a catalyst particle size and the diameter of a CNT formed thereon may be from about 1.2 to about 1.6. One possible theoretical basis for the correlation of particle size and CNT diameter is disclosed in Nasibulin et al., Correlation Between Catalyst Particle and Single-walled Carbon Nanotube Diameters, 43 C
Nucleation of a catalyst may be promoted by the use of light photons (e.g., pulsed laser light, X-ray radiation, ultraviolet, near and far infrared, etc.) such as by passing electromagnetic pulses through the catalyst or through catalyst precursors. This use of laser light may enhance the size uniformity of the resulting catalyst nanoparticles.
During reduction of carbon oxides to form CNTs, such as in the reactions shown in Equations 1 through 6, above, each CNT formed may raise a particle of catalyst material from a surface of bulk catalyst material. Without being bound by any particular theory, it appears that the catalyst surface is slowly consumed by the formation of CNTs due to embedding a particle of the catalyst material into growth tips of the CNTs. The material on which a CNT grows may not be considered a catalyst in the classical sense, but is nonetheless referred to herein and in the art as a “catalyst,” because the carbon is not believed to react with the material. Furthermore, CNTs may not form at all absent the catalyst.
As an alternative theory, the reaction may occur because of the presence of carbon in the catalyst material. Without being bound by any particular theory, carbon may act as a nucleating site for the reaction to proceed. Thus, the carbon in the catalyst material may promote reactions to reduce carbon oxides to solid carbon. As layers of solid carbon are formed, the newly formed carbon material may operate as nucleating sites for subsequent layers of solid carbon products.
The catalyst may include any of groups 5 through 10 of the periodic table (e.g., nickel, molybdenum, chromium, cobalt, tungsten, manganese, ruthenium, platinum, iridium, etc.), as well as lanthanides, actinides, alloys, and other combinations thereof. Catalysts formed from mixtures (e.g., alloys) of these materials may be designed to yield the desired solid carbon morphology.
Various commercially available grades of nickel, molybdenum, platinum, chromium, cobalt, and tungsten, and alloys thereof may be useful as catalysts. Various grades of chromium-, molybdenum-, cobalt-, tungsten-, or nickel-containing alloys or superalloys may be used, for example materials commercially available from Special Metals Corp., of New Hartford, N.Y., under the trade name INCONEL®, or materials commercially available from Haynes International, Inc., of Kokomo, Ind., under the trade name HASTELLOY® (e.g., HASTELLOY® B-2, HASTELLOY® B-3, HASTELLOY® C-4, HASTELLOY® C-2000, HASTELLOY® C-22, HASTELLOY® C-276, HASTELLOY® G-30, HASTELLOY® N, or HASTELLOY® W). The catalyst may be in solid form, such as plates, cylinders, pellets, spheres of various diameters (e.g., as steel shot), or combinations thereof. In some embodiments, catalyst materials may include a stainless steel, such as 15-5 stainless steel, an alloy having 14.0-15.5% Cr, 3.5-5.5% Ni, 2.5-4.5% Cu, 0.15-0.45 Nb+Ta, up to 1.0% Mn, up to 1.0% Si, up to 0.30% S, up to 0.07% C, and up to 0.04% P.
In one embodiment, substantially spherical catalyst material may be used in conjunction with a fluidized-bed reactor. The morphology of CNTs grown on metal catalyst may be dependent on the chemistry of the metal catalyst and the way the catalyst was processed. For example, CNT morphology may be related to grain size and grain boundary shapes within the metal. For example, the characteristic size of these features may influence the characteristic diameter of CNTs formed in the presence of such metal catalysts.
The grain size of a catalyst material may at least partially determine the size of the CNT product. Metals with smaller grain sizes may produce smaller diameter CNTs. The grain size may be a function both of the chemistry of the metal catalyst and the heat-treating methods under which the grains are formed. As used herein, the term “grain size” of a non-ferrous catalyst refers to the mean, median, or mode grain diameter or width of the non-ferrous catalyst surface. For example, cold rolled, hot rolled, precipitation hardened, annealed, case hardened, tempered, or quenched metals may be selected as the catalyst depending on the desired morphology of the solid carbon.
The grain size of the metal crystalline surface may also at least partially determine the size of the CNT product. The grain distribution, including the crystalline grain size and grain boundaries, may be controlled by methods known in the art. For example, grain size may be controlled by controlling nucleation of the metal, such as by grain refinement or inoculation. Inoculants for promoting nucleation may include titanium, boron, aluminum titanium (Al3Ti), titanium diboride (TiB2), etc.
In general, the grain structure of a metal surface may be changed by methods known in the art. For example, a metal structure may be heated to a temperature sufficient to recrystallize the metal structure to form multiple randomly oriented grains. Alternatively, the metal may be heat-treated or annealed to change the grain structure, grain boundary, and grain size. For example, the metal may be annealed by heating the metal to a temperature above its recrystallization temperature, maintaining the temperature for a period of time, then cooling the metal. As another example, metal may be annealed by heating it for a period of time to allow grains within the microstructure of the metal to form new grains through recrystallization.
Recrystallization is a process in which a metal may be plastically deformed, annealed, or otherwise heat-treated. When the metal is heated, the heat-treatment affects grain growth in the metal structure. The size of a crystalline structure may vary with the temperature above the critical temperature and the time at that temperature. Additionally, a faster cooling rate from the recrystallization temperature may provide a larger maximum undercooling and a greater number of nucleation sites, thus producing a finer-grained metal. Thus, in one embodiment, crystal grain size—and thus, nanotube size—may be controlled by nucleation of the catalyst metal, the temperature of the catalyst heat-treatment, the length of time the catalyst metal is above the crystallization temperature, and the cooling process of the metal.
To form catalyst particles having a relatively finer mean grain size, the catalyst material may be heated to a selected temperature, followed by rapid cooling. In some embodiments, CNT diameter and morphology may be controlled by controlling the method of formation of the catalyst. For example, the use of a cold-rolled metal as a catalyst material may result in a different CNT morphology than the use of hot-rolled metal as a catalyst material.
The grain size and grain boundary of catalyst material may be changed to control the size and morphology of the solid carbon product. For example, catalyst material may be annealed at a temperature range from about 600° C. to about 1,100° C., from about 650° C. to about 1,000° C., from about 700° C. to about 900° C., or from about 750° C. to about 850° C. The resulting grain size may be from about 0.1 μm to about 50 μm, from about 0.2 μm to about 20 μm, from about 0.5 μm to about 5 μm, or from about 1.0 μm to about 2.0 μm. Various heat-treating, annealing, and quenching methods are known in the art of metal preparation, grain growth techniques, and grain refinement. Any of these methods may be used to alter the grain size and grain boundaries of the catalyst surface to control the size and morphology of the resulting solid carbon product.
The catalyst surface may be reduced prior to the reaction of carbon oxides. For example, a reducing gas mixture may be introduced into a reactor maintained at a selected temperature, pressure, and concentration to reduce the surface of the catalyst (i.e., to react with or remove oxidized materials). The grain size and grain boundary of the catalyst material may be controlled by heating the catalyst surface and reducing any oxides at the surface. Maintaining the catalyst surface in a reducing environment for longer periods of time may result in relatively larger grain sizes, and shorter reducing treatments may result in relatively smaller grain sizes. Similarly, lower reducing temperatures may result in smaller grain sizes. Oxidation and subsequent reduction of the catalyst surface may alter the grain structure and grain boundaries. The oxidation and/or reduction temperatures may be in the range from about 500° C. to about 1,200° C., from about 600° C. to about 1,000° C., or from about 700° C. to about 900° C. The resulting grain size may range from about 0.1 μm to about 500 μm, from about 0.2 μm to about 100 μm, from about 0.5 μm to about 10 μm, or from about 1.0 μm to about 2.0 μm.
The grain boundary and the mean grain size of the catalyst surface may be controlled, for example, by sputtering (ion bombardment). As used herein, the term “sputtering” refers to the removal of atoms from a surface by the impact of an ion, neutral atoms, neutrons, or electrons. Sputtering may be used to generate surface roughness of a particular grain boundary on the surface of the catalyst. Grain boundaries formed by sputtering may be advantageous for the reduction reactions of carbon oxides. Sputtering may be used to remove atoms from the surface of the metal catalyst. The ion beam energy may determine the resulting grain structure of the metal catalyst surface. For example, in alloys or oxidized metal surfaces, the energy of the ion beam may determine which atoms on the metal surface are removed. The energy applied during sputtering may be selected to remove only a particular atom in certain alloys. Thus, sputtering may result in a grain boundary having atoms or particles with relatively high surface-binding energies on the surface without atoms that may be removed by a low-energy ion beam. Increasing the ion beam energy may remove atoms and particles with higher surface binding energies from the metal surface. Thus, sputtering may be used to produce surfaces having controlled grain boundaries, mean grain sizes, and grain patterns. Sputtering may be used to control the size and morphology of the solid carbon product by controlling the mean grain size, grain boundary, or grain patterns of the metal catalyst surface.
In some embodiments, the catalyst surface may be controlled by chemical etching to form a catalyst surface of a selected mean grain size and with a selected grain boundary. Etching processes include swabbing, immersion, spraying, or other methods. The type of etchant, the strength of the etchant, and the etching time may affect the surface of the metal catalyst. For example, to etch a non-ferrous metal such as nickel-containing alloys or superalloys, an etchant may include a solution of 5 grams of copper(II) chloride (CuCl2) with 100 ml of ethanol and 100 ml of hydrochloric acid. In some embodiments, nitric acid in various concentrations may be used to etch non-ferrous catalysts. If a non-ferrous catalyst includes cobalt, the catalyst may be etched in a solution of iron(III) chloride (FeCl3) in hydrochloric acid, which may result in removing the cobalt. Thus, use of such an etchant may selectively etch the cobalt from a cobalt alloy, leaving other metals on the surface of the catalyst. In this manner, the grain boundary of the surface may be selectively controlled, thereby enabling control of properties of the solid carbon product formed thereon.
Catalyst material may be secured to a structure and placed in a reactor. Alternatively, the catalyst may be pulverized or ball-milled. The pulverization or ball-milling process may affect the catalyst grain size and grain boundary, thereby affecting the morphology of CNTs formed. The pulverized or ball-milled non-ferrous catalyst may be collected and sieved to increase the uniformity of the catalyst particle size. If the catalyst is in powder or particulate form, the catalyst may be carried into the reactor by a carrier gas or a reactant gas. Catalyst in particulate form may also be used in a fluidized-bed reactor. Dynamic action of metal catalyst particles within the fluidized bed may continually cause fresh catalyst surfaces to be exposed as carbon nanotubes are formed and spalled off of the catalyst particle surface. Catalyst particles may be configured to increase the surface area of the catalyst in contact with the carbon oxide gases and the reducing gases as the reaction proceeds.
Reaction temperatures may depend on the composition of the catalyst or on the size of the catalyst particles. Catalyst materials having small particle sizes tend to catalyze reactions at lower temperatures than the same catalyst materials with larger particle sizes. For example, the Bosch reaction may occur at temperatures in the range of approximately 400° C. to 800° C. for iron-based catalysts, depending on the particle size and composition and the desired solid carbon product. In general, graphite and amorphous solid carbon form at lower temperatures, and CNTs form at higher temperatures. CNTs may form at temperatures above about 680° C. In general, the reactions described herein proceed at a wide range of pressures, from near vacuum, to pressures of 4.0 MPa (580 psi) or higher. For example, CNTs may form in pressure ranges of from about 0.28 MPa (40 psi) to about 6.2 MPa (900 psi). In some embodiments, CNTs may form at pressures from about 0.34 MPa (50 psi) to about 0.41 MPa (60 psi), or at a pressure of about 4.1 MPa (600 psi). Typically, increasing the pressure increases the reaction rate.
Under some conditions, carbon forms a buckysphere around a particle of catalyst, which may partially merge with the tube structure of a CNT, forming a nanobud. The introduction of additional catalyst material after the formation of CNTs may induce the formation of CNTs having branched or bud morphology.
When using a solid catalyst, such as a wafer of metal catalyst, CNTs appear to grow in a series of generations. Without being bound by any particular theory, it appears that reaction gases interact with an exposed surface of catalyst, and CNTs begin to grow on the surface. As the growth continues, neighboring CNTs become entangled and lift particles of the catalyst off the surface, exposing a new layer of catalyst material to the reaction gases. As each layer of catalyst material lifts off of the surface, the CNTs become entangled in clumps that resemble “pillows” or cockleburs under magnification.
A fluidized-bed reactor may take advantage of the detachment of CNTs as a separation means. That is, the flow of gases in a fluidized-bed reactor may be selected such that formations of CNTs are entrained in the gas flow, elutriated from the catalyst surface, and subsequently harvested from the gas mixture leaving the reactor.
Without being bound by any particular theory, carbon may act as a nucleating site for solid carbon. For example, as a component of a catalyst material, carbon may promote the reaction. As the reaction continues and each layer of solid carbon is formed, newly formed carbon may act as a nucleating site for subsequent layers of solid carbon. Thus, in one embodiment, the size and morphology of the solid carbon product is controlled by selecting and controlling the carbon composition of the catalyst metal.
A catalyst composition in which catalyst layers are consumed during a reaction may expose fresh surfaces of catalyst, allowing for the formation of solid carbon products to continue uninterrupted. Without being bound by any particular theory, such a mechanism appears to occur, for example, when rusted steel is used as the solid metal catalyst.
As depicted in, for example,
CNT pillow formations may form into larger agglomerations. For example, if a sample of carbon nanotube pillows is gently stirred or shaken in ethanol, the pillows agglomerate and interlock so that the boundaries of the pillows become indistinct. The agglomerations may be larger and stronger than the individual pillow formations. The pillow morphology of CNTs may be particularly suitable for forming various types of carbon nanotube paper, felts, electrodes, etc.
Various reactor designs may facilitate the formation and collection of desired solid carbon products. For example, a reactor may be designed to increase the surface area of a non-ferrous catalyst exposed to carbon oxides and reducing gases. In some embodiments, the reactor may be designed to accommodate catalyst particles having a relatively small mean diameter, thereby increasing the exposed catalyst surface area per unit mass of catalyst material. The reactor may be configured to hold layered sheets of catalyst material. In such embodiments, the exposed surface area per unit volume may be optimized, such as in configurations similar to radiator configurations. The reactor may also be designed to promote the breaking off of the solid carbon products from the non-ferrous catalyst surface, such as by the flow of reaction gases. The reactor may further be designed to promote elutriation of solid carbon products out of the reactor with excess reactant gases or a carrier gas, enabling continuous operation of the reactor.
Aerosol and fluidized-bed reactors are well suited for high-volume continuous production of solid carbon products. A fluid-wall reactor has the advantages of providing for the introduction of various substances (catalysts, additional reactants) and of minimizing or eliminating the accumulation of solid carbon products on reactor walls.
In some embodiments, a non-ferrous catalyst material may be conditioned before reduction of carbon oxides. A reactor volume may be purged or displaced by a reducing agent, and the temperature of the reactor may be controlled to reduce any oxides on the catalyst surface. The reactor temperature, the reducing time, and the reducing gas temperature and pressure may be controlled to control the grain size and grain boundary of the catalyst surface, as described above. Altering the grain size and grain boundary of the catalyst surface may alter the size and morphology of the carbon nanotube product. For example, the reducing gas and reactor may range from about 500° C. to about 1,200° C., from about 600° C. to about 1,000° C., or from about 700° C. to about 900° C. The catalyst may be exposed to the reducing agent for a period of time sufficient to reduce any oxides. After conditioning of the catalyst, a reaction gas mixture including a carbon oxide may be introduced into the reactor, and the reactor temperature and pressure may be maintained to suitable conditions for the reduction of the carbon oxide to form a desired solid carbon product.
In some embodiments, the reactor may be an aerosol reactor in which the catalyst is formed in a gas phase or in which the catalyst is preformed and selected for a specific size distribution, mixed into a liquid or carrier gas solution, and then sprayed into the reactor (e.g., via electrospray). The catalyst may then remain distributed in the gas phase or be deposited on solid surfaces in the reaction zone for the growth phase of the carbon product. The catalyst may subsequently transport the product out of the reaction zone. In another embodiment, one or more reactors may be fluidized-bed reactors in which the catalyst or catalyst-coated particles are introduced into the reactor and the solid carbon product is grown on the surface of the particles. The solid carbon may be either elutriated in the reactor, and carried out of the reactor entrained in the reaction gases, or the catalyst particles may be harvested and the solid carbon removed from the surface.
In some embodiments, a reactor is configured such that reactant gases enter at or near the top of the reactor and exit at or near the bottom of the reactor. The catalyst may be placed in the reactor to maximize the surface area of exposed catalyst per unit volume of reactor. For example, the catalyst may be in thin sheets, and the reactor may be configured to receive multiple sheets of catalyst material. The catalyst sheets may be arranged such that reactant gases flow past each sheet of catalyst material before exiting the reactor. For example, the catalyst sheets may be staggered in the reactor, such that the reactant gases flow across a first plate at the top of the reactor, past the first plate at the side of the reactor, then past the bottom of the first plate and the top of the second plate toward an opposite side of the reactor. This process may continue as the reactant gases pass through the reactor. The solid carbon product may be collected at the bottom of the reactor. The downward flow of the reactant gases and downward gravitational forces may promote the removal of solid carbon products from the surface of the catalyst.
The reactors may be batch reactors in which the catalyst is either a fixed solid surface or is mounted on a fixed solid surface (e.g., catalyst nanoparticles deposited on an inert substrate), with the solid carbon grown on the catalyst, and the catalyst and solid carbon product periodically removed from the reactor. Alternatively, the reactors may be continuous, wherein a solid catalyst or catalyst mounted on a solid substrate passes through a flowing gas stream, the resulting solid carbon product is harvested, and the solid surface is reintroduced to the reactor. The solid substrate may be the catalyst material (e.g., a solid piece of a chromium-, molybdenum-, cobalt-, or nickel-containing alloy or superalloy) or a surface on which the catalyst is mounted.
In one embodiment, a fluidized-bed reactor may be designed to retain the catalyst while allowing the solid CNT product to be entrained in the gas flow and to be lofted out of the reaction zone upon reaching a desired size. The shape of the reactor, the gas flow rates, or shape and flow rates in combination may control the residence time of the elutriates and the corresponding size of the solid carbon product (such as the length of the carbon nanotubes).
In one embodiment, particles in a fluidized-bed reactor are of a substantially uniform diameter. The diameter of the catalyst in the fluidized bed may be chosen based on the particular reactor configuration, the flow rate of the reactants through the reactor, the shape of the catalyst, the density of the catalyst, and the density of the reactant gases and any inert carrier gases. The diameter of the catalyst particles may be chosen to avoid entrainment of the catalyst with the reaction product and also to avoid channeling of the reactants through the bed. A diffuser or sparger may distribute the gaseous reactants to provide a uniform flow pattern through the bed particles and limit or prevent channeling of gases through the particle bed.
When the catalyst is a sheet or plate over an object of manufacture, the entire surface of the object of manufacture need not be uniformly coated with the carbon product. The carbon deposition area on the solid surface optionally may be limited to one or more regions by masking, or by selectively depositing the catalyst to promote the formation of the solid carbon on portions of the solid surface.
Solid carbon products may be collected and separated from the gas stream or from solid surfaces on which they form, such as by elutriation, centrifugation, electrostatic precipitation, or filtration. The techniques for separation of the solid product from the gas stream and the catalyst may depend on the type of reactor. For example, the solid carbon product may be harvested directly from a gas stream using electrophoretic or thermophoretic collectors, filters, etc., or by collecting the elutriates as they exit the reactor. After harvesting solid carbon products, gases may be recycled through the reactor. Combining the catalytic conversion process with a separation process may be beneficial because such a carbon separation and sequestration unit may be more economical than conventional separation and sequestration methods.
The catalytic converters described herein may use carbon oxides at relatively low pressures, so that equipment and costs associated with compression, liquefaction, and transport may be reduced. Furthermore, the heat produced in the catalytic converters may provide at least some of the process heat for the separation process. For example, a separation process, such as amine absorption, may receive at least part of the heat required for desorption from the catalytic converter, and deliver low pressure carbon oxide gases to the catalytic converter.
In one embodiment, a cyclone separator is used to separate and collect the solid carbon product. For a solid catalyst or solid surface-mounted catalyst, the solid carbon product may be scraped or otherwise abraded from the surface of the solid carrier material. Alternatively, when using a solid catalyst, the solid carbon product may be rinsed off a surface with a solvent for further processing.
In some cases, it may be beneficial to remove the solid carbon product from the reaction gas mixture prior to cooling (e.g., by withdrawing the solid carbon product from the reactor through a purge chamber wherein the reaction gases are displaced by an inert purging gas such as argon, nitrogen, or helium). Purging prior to cooling helps reduce the deposit or growth of undesirable morphologies on the desired solid carbon product during the cooling process.
In aerosol or fluidized-bed reactors, the residence time in the growth zone may be controlled by one or more forces (such as gravitational, electromagnetic, or centrifugal forces) counteracting the motion of the gas stream. These forces counterbalance the gas flow to help control the residence time, so that the size of the solid carbon product may be controlled.
In another embodiment, catalysts are introduced into an aerosol reactor by an electrospray process. Coulomb forces separate a suspension or solution containing a catalyst powder into small droplets from which individual particles form. The electrospray helps keep the particles separated so that they do not tend to clump or fuse. The electrospray also tends to charge the resulting carbon particles and make them easier to harvest from the aerosol using electrostatic collectors.
In aerosol reactors, catalyst particles may be sprayed into a carrier gas or fluid for transport into the reaction zone. The catalyst may be preconditioned in a catalyst-conditioning process prior to mixing with the reaction gases. Catalyst conditioning by heating in an inert carrier gas may promote the growth of specific chiralities of single wall CNTs. For example, heating catalyst material in a helium environment may promote the growth of chiralities of CNTs having metallic properties. One or more substances may be introduced into the reaction zone to modify the physical properties of the desired solid carbon product, either through incorporation in the solid carbon product, or by surface deposition on the solid carbon product.
The physical properties of the solid carbon products may be substantially modified by the application of additional substances to the surface of the solid carbon. Modifying agents (e.g., ammonia, thiophene, nitrogen gas, and/or surplus hydrogen) may be added to the reaction gases to modify the physical properties of the resulting solid carbon. Modifications and functionalizations may be performed in the reaction zone or after the solid carbon products have been removed.
Some modifying agents may be introduced into the reduction reaction chamber near the completion of the solid carbon formation reaction by, for example, injecting a water stream containing a substance to be deposited, such as a metal ion. The substances may also be introduced as a component of a carrier gas. For example, surplus hydrogen may cause hydrogenation of a carbon lattice in some CNTs, causing the CNTs to have semiconductor properties.
Small amounts of substances (e.g., sulfur) added to the reaction zone may be catalyst promoters that accelerate the growth of carbon products on the catalysts. Such promoters may be introduced into the reactor in a wide variety of compounds. Such compounds may be selected such that the decomposition temperature of the compound is below the reaction temperature. For example, if sulfur is selected as a promoter for an iron-based catalyst, the sulfur may be introduced into the reaction zone as a thiophene gas, or as thiophene droplets in a carrier gas. Examples of sulfur-containing promoters include thiophene, hydrogen sulfide, heterocyclic sulfides, and inorganic sulfides. Other catalyst promoters include volatile lead, bismuth compounds, ammonia, nitrogen, excess hydrogen (i.e., hydrogen in a concentration higher than stoichiometric), and combinations of these.
In some embodiments, a catalyst particle is removed from the surrounding matrix as a CNT grows, and the catalyst particle may become embedded in one of the ends of the CNT. Thus, some of the catalyst material may be physically removed during the reaction, and the catalyst may need to be continually replenished. The material on which a CNT grows may not be considered a catalyst in the classical sense, but is nonetheless referred to herein and in the art as a “catalyst,” because the carbon is not believed to react with the material. Furthermore, CNTs may not form at all absent the catalyst. In scanning electron microscope images, catalyst ends appear significantly larger (e.g., 1.2 to 1.6 times the diameter) than the tubes that grow from them. This difference may be due to a carbon shell surrounding the catalyst, it may be indicative of a fundamental relationship between the catalyst particle size and that of the CNT that grows from it, or it may be due to some other factor or coincidence. Whatever the reason, one way to control the size of the CNTs appears to be through the control of the catalyst particle size, or grain size, keeping the catalyst particle size somewhat larger than the desired nanotube size.
The methods disclosed herein may be incorporated into power production, chemical processes, and manufacturing processes in which the combustion of a primary hydrocarbon fuel source is the primary source of heat. The resulting combustion gases from such processes contain carbon oxides that may act as sources of carbon for the manufacture of the desired solid carbon product. The methods are scalable for many different production capacities so that, for example, plants designed with this method in mind may be sized to handle the carbon oxide emissions from the combustion processes of a large coal-fired power plant or those from an internal combustion engine. For example, the methods may be used to reduce carbon dioxide from the atmosphere, combustion gases, process offgases, exhaust gases from the manufacture of Portland cement, and well gases, or from separated fractions thereof.
In another embodiment, the carbon oxides from a source gas mixture are separated from the source mixture and concentrated to form the carbon oxide feedstock for the reduction process. The carbon oxides in the source gases may be concentrated through various means known in the art. In yet another embodiment, the catalytic conversion process may be employed as an intermediate step in a multi-stage power extraction process wherein the first stages cool the combustion gases to the reaction temperature of the reduction process for the formation of the desired solid carbon product. The cooled combustion gases, at the desired temperature of the reduction reaction, may then be passed through the reduction process and subsequently passed through additional power extraction stages.
Coupling this method with a hydrocarbon combustion process for electrical power production has an additional advantage in that the hydrogen required for the reduction process may be formed by the electrolysis of water using off-peak power. The oxygen formed in the electrolysis process may be used as at least a portion of the combustible mixture for the combustion process.
When the methods disclosed herein are coupled with a combustion or chemical process that uses hydrocarbons, a portion of the hydrocarbons of the process may be used as the reducing agent gas. This may include the pyrolysis of the hydrocarbons to form a hydrogen gas that is provided as the reducing agent gas. The process of this disclosure may be adapted to various available hydrocarbon sources.
The reduction process of this method results in the formation of solid carbon product and water. The water may subsequently be condensed and the latent heat extracted for heating purposes, or as part of a low-pressure power extraction cycle. The water may be extracted as a useful co-product, and the associated latent heat of the water may be used for another process.
The following examples illustrate the processes described. Each example is explained in additional detail in the following subsection, and scanning electron microscope images of products of some examples are included.
The laboratory setup for all the examples is illustrated in
The gases used in various combinations in the examples were: research grade carbon dioxide (CO2), available from PraxAir; research grade methane (CH4), available from PraxAir; standard grade nitrogen (N2), available from PraxAir; research grade helium (He), available from Air Liquide; and research grade hydrogen (H2), available from PraxAir.
As depicted in
The temperature of the first tube furnace 1 was measured by a type-K thermocouple located inside the outer quartz shell at approximately the centerline of the first tube furnace 1. The temperature of the second tube furnace 2 was measured by a type-K thermocouple located at approximately the centerline of the second tube furnace 2 in a well drilled in the ceramic insulation of the tube furnace 2. The temperatures are reported as shown on these thermocouples.
No attempt was made to measure or to control the recirculation flow rate, and the quality of the product and speed of reaction seemed to be independent of flow rate (e.g., whether a high-volume compressor or a low-volume pump were used). Without being bound by any particular theory, the flow rates may have all been above a critical threshold. Flow rates may be important for design and operation of production facilities, but are not particularly important in the tests reported herein because the volume of the experimental apparatus was much larger than the volume of the catalyst and resulting solid carbon product. Appropriate tests to determine the optimum flow rates for a specific production design will readily occur to a skilled practitioner.
During the experiments, the pressure of the gases in the experimental apparatus would suddenly begin to rapidly drop as the temperature increased. The temperature at which the pressure began to drop varied with the catalyst and gas mixture. This drop in pressure may be an indication of the onset of formation of the solid carbon product. When the pressure dropped, additional reaction gases were added to the experimental apparatus via the mixing valve 7 to maintain pressure. After a short time, the pressure would begin to rise, at which point the mixing valve 7 was closed. The magnitude and duration of the pressure drop appear to be an indication of the onset of CNT growth and/or the rate of growth.
The start-up procedure followed one of two methods: heating the experimental apparatus in an inert gas (helium or nitrogen), or heating the experimental apparatus in air. In the case of heating in the inert gas, the experimental apparatus was evacuated and purged by the vacuum pump 5 for approximately five minutes, after which the vacuum pump 5 was turned off and isolated. The experimental apparatus was brought to atmospheric pressure with the inert gas. The inert gas was then turned off, and the heating elements of the tube furnaces 1, 2 were turned on to begin the heating cycle. In the case of air, the tube furnaces 1, 2 were not purged at start-up, and were simply brought up to operating temperature.
When the furnaces reached approximately the experimental set point temperature, the experimental apparatus was evacuated and purged with a reaction gas mixture (typically a stoichiometric mixture of carbon dioxide and reducing gas) for five minutes. The experimental apparatus was then brought to atmospheric pressure while the reaction gases and the temperature continued to rise and until the experimental apparatus gauge temperature was at the selected test temperature.
In the examples, the tube furnaces 1, 2 were operated for a fixed time (typically 1 hour), after which the tube furnaces 1, 2 were turned off. After the tube furnaces 1, 2 were turned off, the vacuum pump 5 was turned on, the reaction gases evacuated and the experimental apparatus purged with an inert gas (either helium or nitrogen) for approximately five minutes. Then the vacuum pump 5 was turned off and the experimental apparatus was brought up to atmospheric pressure with an inert purge gas and allowed to cool.
During the experiments, there were no observed differences in the quality of the CNTs produced based on the inert gas used for purging and cooling. Implementations of continuous flow reactors based on the examples herein will readily occur to a skilled practitioner.
A sample of mild steel wafer with extensive red rust spots was used as the catalyst. The mild steel wafer was placed in the tube furnace 1 at approximately the centerline. The vacuum pump 5 was started, and helium was used to purge the experimental apparatus for five minutes. After five minutes, the vacuum pump 5 was turned off, the compressor 3 was turned on, the refrigerated condenser 4 was turned on, and the helium gas continued to flow until the pressure reached 90.6 kPa (680 Torr), at which point the gas flow was shut off. The heating element of the tube furnace 1 was then turned on.
When the furnace 1 temperature reached a temperature of 680° C., the vacuum pump 5 was turned on, and reaction gases in a stoichiometric mixture of carbon dioxide and hydrogen (delivered from the gas supply 6 by the mixing valve 7) were used to purge the experimental apparatus for five minutes. After five minutes, the vacuum pump 5 was turned off. When the experimental apparatus reached a pressure of 101.3 kPa (760 Torr), the mixing valve 7 was closed to stop the flow of reaction gases into the tube furnace 1. The compressor 3 and the refrigerated condenser 4 were operating to circulate the reaction gases through the tube furnaces 1, 2. Additional reaction gases were added by periodically opening the mixing valve 7 to keep the experimental apparatus gauge pressure between 85.3 kPa (640 Torr) and 101.5 kPa (760 Torr). The reaction gases circulated through the tube furnaces 1, 2 for one hour, after which the heating element of the furnace 1 was shut off, the vacuum pump 5 was started, and the experimental apparatus was purged with helium for five minutes from gas supply 6 controlled by mixing valve 7. The vacuum pump 5 was then shut off and the helium purge gas continued to flow until the gauge pressure in the experimental apparatus was 98.7 kPa (740 Torr). The furnace 1 was then left to cool.
The steel sample was removed after the furnace 1 had cooled.
A quartz disk was placed lying flat on a wafer of 304 stainless steel, which was used as the catalyst. The wafer was placed in furnace 1 at approximately the centerline. The experimental apparatus was helium-purged and heated as in Example 1. Reaction gases were added and recirculated for one hour at a temperature of 680° C. and a pressure between 85.3 kPa (640 Torr) and 101.3 kPa (760 Torr), as in Example 1.
The stainless steel sample was removed from the furnace 1 after the furnace 1 had cooled. A mat of CNTs had grown between the quartz and the stainless steel wafer. Portions of the CNT mat adhered to both the quartz and the stainless steel surfaces.
A wafer of 316L stainless steel was used as the catalyst. The 316L stainless steel wafer was placed in furnace 1 at approximately the centerline. The experimental apparatus was helium-purged and heated as in Example 1. Reaction gases were added and recirculated for one hour as in Example 1, but at a temperature of 700° C. and a pressure between 93.3 kPa (700 Torr) and 97.3 kPa (730 Torr).
The stainless steel wafer was removed from the furnace 1 after the furnace 1 had cooled.
A sample of mild steel wool was used as the catalyst. The steel wool was placed in the furnace 1 near the centerline and heated in air. The compressor 3, the refrigerated condenser 4, and the heating element of the tube furnace 1 were turned on, circulating air through the experimental apparatus. When the furnace 1 temperature reached 645° C., the vacuum pump 5 was started, and a stoichiometric mixture of carbon dioxide and hydrogen flowed from the gas supply 6 (via the mixing valve 7) into the tube furnace 1 for five minutes. The temperature of the furnace 1 continued to increase to a set point of 700° C. At the end of five minutes, the vacuum pump 5 was shut off and the gases continued to flow until the gauge pressure of the experimental apparatus was 70.6 kPa (530 Torr), at which point the reaction gas flow rate was reduced to a lower flow rate sufficient to keep the pressure between 66.6 kPa (500 Torr) and 70.6 kPa (530 Torr). The reaction gases circulated through the tube furnaces 1, 2 for one hour, after which the heating element of furnace 1 was shut off, the vacuum pump 5 was started, and the experimental apparatus was purged with helium for five minutes. The vacuum pump 5 was then shut off, and the helium purge gas continued to flow until the gauge pressure in the experimental apparatus was 93.3 kPa (700 Torr). The furnace 1 was then left to cool.
The steel wool sample with the solid carbon product was removed after the furnace 1 had cooled.
A sample of 316 stainless steel wire was used as the catalyst. The wire was placed in the furnace 1 near the exit of the furnace 1. The heating element of the furnace 1, the refrigerated condenser 4, and the vacuum pump 5 were turned on. Reaction gases in a stoichiometric mixture of carbon dioxide and hydrogen (delivered from the gas supply 6 by the mixing valve 7) were used to purge the experimental apparatus for five minutes. After five minutes, the vacuum pump 5 was turned off, the compressor 3 was turned on, and the reaction gas mixture continued to flow until the gauge pressure of the experimental apparatus was 78.5 kPa (589 Torr), at which point the reaction gas flow was shut off. The reaction gases circulated through the tube furnaces 1, 2 for two hours at 575° C., after which the heating element of the furnace 1 was shut off, the vacuum pump 5 was started, and the experimental apparatus was purged with helium for five minutes. The vacuum pump 5 was then shut off, and the helium continued to flow until the gauge pressure in the experimental apparatus was 93.3 kPa (700 Torr). The furnace 1 was then left to cool.
The steel wire was removed from the furnace 1 after the furnace 1 had cooled.
A wafer of 304 stainless steel was used as the catalyst. Quartz discs were place on the upper surface of the stainless steel wafer. The stainless steel wafer and quartz discs were placed in the furnace 1 at approximately the centerline. The experimental apparatus was helium-purged and heated as in Example 1. Reaction gases were added and recirculated at a temperature of 650° C. and a pressure between 85.3 kPa (640 Torr) and 101.3 kPa (760 Torr), as in Example 1.
The stainless steel wafer and quartz discs were removed after the furnace 1 had cooled.
Substitution of the catalyst in the previous examples with catalysts comprised of groups 5 through 10 of the periodic table (e.g., nickel, molybdenum, chromium, cobalt, tungsten, manganese, ruthenium, platinum, iridium, etc.), actinides, lanthanides, and alloys and other combinations thereof may yield substantially similar results. Thus, substitution of catalyst with a chromium-, molybdenum-, cobalt-, tungsten-, or nickel-containing alloy or superalloy may yield a substantially similar result, with the size and morphology of the nanotube product dependent on the grain size of the catalyst material. Catalysts may also include mixtures of such metals. Similar reaction conditions as those described herein may be used with such catalysts. For example, the reaction temperature may range from about 500° C. to about 1,200° C., from about 600° C. to about 1,000° C., or from about 700° C. to about 900° C. In some embodiments, the temperature may be at least 650° C., such as at least 680° C., to produce a selected solid carbon product. The size and morphology of the solid carbon product (e.g., CNTs) may depend on the grain size of the non-ferrous catalyst.
For Examples 7 through 39 below, metal coupons were cut from a sheet of material, or another metal was catalyst was used as indicated. Coupons were generally approximately 13 mm to 15 mm wide, approximately 18 mm to 22 mm long, and approximately 2 mm to 6 mm thick. Coupons were separately placed in quartz boats about 8.5 cm long and 1.5 cm wide, and the boats were inserted end-to-end into a quartz tube having an inner diameter of about 2.54 cm and a length of about 1.2 m. The quartz tube was then placed in a tube furnace. The quartz tube was purged with hydrogen gas to reduce the surface of the coupons before the tube furnace was heated to operating conditions. After the tube furnace reached operating conditions, reaction gases were introduced into the quartz tube (i.e., flowed continuously through the quartz tube) such that both the upper and lower surfaces of each coupon were exposed to reaction gas. The temperature, pressure, and gas composition were measured at each coupon. After the test, the coupons were removed from the quartz tube. Weight changes and carbon formation were noted.
Three coupons were cut from a sheet of 304H stainless steel, and were washed in hydrochloric acid to remove contaminants and oxidation. The coupons were placed in quartz boats in a quartz tube as described above. A reaction gas containing about 50% H2 and 50% CO was introduced into the quartz tube at about 4.0 MPa. The gases flowed over the coupons for about 4 hours at 2000 sccm (standard cubic centimeters per minute). Solid carbon formed on each coupon at the rates shown in Table 2 below. Methane, carbon dioxide, and water were also formed in the quartz tube. After the test, solid carbon was physically removed from the coupons and tested for BET specific surface area, as shown in Table 2. Samples of the solid carbon were imaged using SEM, as shown in
Three coupons were cut from a sheet of 25-35MA stainless steel (an alloy having 23%-27% Cr, 33%-37% Ni, 1.5% Mn, 2.0% Si, 0.35%-0.55% C, 0.50%-1.25% Nb, up to 0.50% Mo, with the balance Fe, available from MetalTek International, of Waukesha, Wis.) and were washed in hydrochloric acid to remove contaminants and oxidation. The coupons were placed in quartz boats in a quartz tube as described above. A reaction gas containing about 50% H2 and 50% CO was introduced into the quartz tube at about 4.0 MPa. The gases flowed over the coupons for about 4 hours at 2000 sccm. Solid carbon formed on each coupon at the rates shown in Table 3 below. Methane, carbon dioxide, and water were also formed in the quartz tube. After the test, solid carbon was physically removed from the coupons and tested for BET specific surface area, as shown in Table 3. Samples of the solid carbon were imaged using SEM, as shown in
Three coupons were cut from a sheet of 25-35MA stainless steel and were washed in hydrochloric acid to remove contaminants and oxidation. The coupons were placed in quartz boats in a quartz tube as described above. A reaction gas containing about 50% H2 and 50% CO was introduced into the quartz tube at about 4.0 MPa. The gases flowed over the coupons for about 4 hours at 2000 sccm. Solid carbon formed on each coupon at the rates shown in Table 4 below. Methane, carbon dioxide, and water were also formed in the quartz tube. After the test, solid carbon was physically removed from the coupons and tested for BET specific surface area, as shown in Table 4. Samples of the solid carbon were imaged using SEM, as shown in
Three coupons were cut from a sheet of Super 20-32Nb stainless steel (an alloy having 20% Cr, 33% Ni, 1.25% Mn, 0.60% Si, up to 0.12% C, 0.50%-1.25% Nb, up to 0.50% other materials, with the balance Fe, available from MetalTek International, of Waukesha, Wis.) and were washed in hydrochloric acid to remove contaminants and oxidation. The coupons were placed in quartz boats in a quartz tube as described above. A reaction gas containing about 50% H2 and 50% CO was introduced into the quartz tube at about 4.0 MPa. The gases flowed over the coupons for about 4 hours at 2000 sccm. Solid carbon formed on each coupon at the rates shown in Table 5 below. Methane, carbon dioxide, and water were also formed in the quartz tube. After the test, solid carbon was physically removed from the coupons and tested for BET specific surface area, as shown in Table 5. Samples of the solid carbon were imaged using SEM, as shown in
Three coupons were cut from a sheet of HAYNES® 230 alloy (an alloy having 22% Cr, 57% Ni, 14% W, 2% Mo, 3% Fe, 5% Co, 0.5% Mn, 0.4% Si, 0.3% Al, 0.10% C, 0.02 La, and 0.015% B, available from Haynes International, of Kokomo, Ind.) and were washed in hydrochloric acid to remove contaminants and oxidation. The coupons were placed in quartz boats in a quartz tube as described above. A reaction gas containing about 50% H2 and 50% CO was introduced into the quartz tube at about 4.0 MPa. The gases flowed over the coupons for about 4 hours at 2000 sccm. Solid carbon formed on each coupon at the rates shown in Table 6 below. Methane, carbon dioxide, and water were also formed in the quartz tube. After the test, solid carbon was physically removed from the coupons and tested for BET specific surface area, as shown in Table 6. Samples of the solid carbon were imaged using SEM, as shown in
Three coupons were cut from a sheet of HAYNES® HR-160 alloy (an alloy having 28% Cr, 37% Ni, 29% Co, 2% Fe, 2.75% Si, 0.5% Mn, 0.5% Ti, 0.05% C, and up to 1% each of W, Mo, Nb, available from Haynes International, of Kokomo, Ind.) and were washed in hydrochloric acid to remove contaminants and oxidation. The coupons were placed in quartz boats in a quartz tube as described above. A reaction gas containing about 50% H2 and 50% CO was introduced into the quartz tube at about 4.0 MPa. The gases flowed over the coupons for about 4 hours at 2000 sccm. Solid carbon formed on each coupon at the slow reaction rates shown in Table 7 below. Methane and carbon dioxide were formed in only small amounts. After the test, samples of the solid carbon were imaged using SEM, as shown in
Three coupons were cut from a sheet of NICROFER® 6025HT alloy (an alloy having 24%-26% Cr, 8%-11% Fe, 0.15%-0.25% C, up to 0.5% Mn, up to 0.5% Si, up to 0.10% Cu, 1.8%-2.4% Al, 0.10%-0.20% Ti, 0.05%-0.12% Y, 0.01%-0.10% Zr, up to 0.02% P, up to 0.1% S, and the balance Ni, available from ThyssenKrupp VDM, of Werdohl, Germany) and were washed in hydrochloric acid to remove contaminants and oxidation. The coupons were placed in quartz boats in a quartz tube as described above. A reaction gas containing about 50% H2 and 50% CO was introduced into the quartz tube at about 4.0 MPa. The gases flowed over the coupons for about 4 hours at 2000 sccm. Solid carbon formed on each coupon at the slow reaction rates shown in Table 8 below. Methane and carbon dioxide were formed in only small amounts. After the test, solid carbon was physically removed from the coupons and samples of the solid carbon were imaged using SEM, as shown in
Three coupons were cut from a sheet of ASTM F321 alloy (i.e., an alloy having 0.08% C, 2.0% Mn, 0.45% P, 0.030% S, 1.0% Si, 9.0%-12.0% Ni, 17.0%-19.0% Cr, with the balance Fe, in accordance with ASTM Standard A182) and were washed in hydrochloric acid to remove contaminants and oxidation. The coupons were placed in quartz boats in a quartz tube as described above. A reaction gas containing about 50% H2 and 50% CO was introduced into the quartz tube at about 4.0 MPa. The gases flowed over the coupons for about 4 hours at 2000 sccm. Solid carbon formed on each coupon at the rates shown in Table 9 below. Methane, carbon dioxide, and water were also formed in the quartz tube. After the test, solid carbon was physically removed from the coupons and tested for BET specific surface area, as shown in Table 9. Samples of the solid carbon were imaged using SEM, as shown in
Twelve coupons were cut from a sheet of INCONEL® 693 alloy (i.e., an alloy having 27%-31% Cr, 2.5%-6.0% Fe, 2.5%-4.0% Al, 0.5%-2.5% Nb, up to 1.0% Mn, up to 1.0% Ti, up to 0.5% Cu, up to 0.5% Si, up to 0.15% C, up to 0.01% S, with the balance Ni, available from Special Metals Corporation, of New Hartford, N.Y.) and were washed in hydrochloric acid to remove contaminants and oxidation. The coupons were placed in quartz boats in a quartz tube as described above. A reaction gas containing about 50% H2 and 50% CO was introduced into the quartz tube at about 4.0 MPa. The gases flowed over the coupons for about 5 hours at 2000 sccm. Solid carbon formed on the coupon at the rates shown in Table 10 below. Methane, carbon dioxide, and water were also formed in the quartz tube. After the test, solid carbon was physically removed from the coupons and imaged using SEM, as shown in
An alonized stainless steel tube was placed in a tube furnace without any coupons inside. The tube was purged with hydrogen gas to reduce the surface of the tube before the tube furnace was heated to operating conditions. After the tube furnace reached operating conditions, a reaction gas containing about 50% H2 and 50% CO was introduced into the tube at about 4.0 MPa. The gases flowed inside the tube for about 4 hours at 2000 sccm. Solid carbon formed on the interior of the tube between a point 24 inches (60 cm) from the gas inlet and 28 inches (71 cm) from the gas inlet. Methane, carbon dioxide, and water were also formed in the quartz tube. After the test, about 2.21 g of solid carbon were collected from the tube. Samples of the solid carbon were tested for BET surface area as shown in Table 11. Samples were imaged using SEM, as shown in
A tube formed of KANTHAL® alloy (an alloy of iron, chromium, and aluminum, available from Sandvik Materials Technology, of Sandviken, Sweden) was placed in a tube furnace without any coupons inside. The tube was purged with hydrogen gas to reduce the surface of the tube before the tube furnace was heated to operating conditions. After the tube furnace reached operating conditions, a reaction gas containing about 50% H2 and 50% CO was introduced into the tube at about 4.0 MPa. The gases flowed inside the tube for about 4 hours at 2000 sccm. Very little solid carbon formed on the interior of the tube between a point 10 inches (25 cm) from the gas inlet and 33 inches (84 cm) from the gas inlet. Methane, carbon dioxide, and water formed in the tube in small amounts. After the test, about 0.1 g of solid carbon were collected from the tube. A sample of the solid carbon was imaged using SEM, as shown in
Twelve coupons were cut from a sheet of galvanized steel (i.e., mild steel treated with zinc oxide) and were washed in ethanol to remove contaminants and oxidation. The coupons were placed in quartz boats in a quartz tube as described above. A reaction gas containing about 45% H2 and 45% CO and 10% Ar was introduced into the quartz tube at about 4.0 MPa. The gases flowed over the coupons for about 4 hours at 1200 sccm. Solid carbon formed on each coupon at the rates shown in Table 13 below. Methane, carbon dioxide, and water were also formed in the quartz tube. After the test, solid carbon was physically removed from the coupons and tested for BET surface area, as shown in Table 13. Samples of the solid carbon were imaged using SEM, as shown in
Twelve coupons were cut from a sheet of copper and were washed in ethanol to remove contaminants and oxidation. The coupons were placed in quartz boats in a quartz tube as described above. A reaction gas containing about 45% H2 and 45% CO and 10% Ar was introduced into the quartz tube at about 4.0 MPa. The gases flowed over the coupons for about 4 hours at 1200 sccm. Solid carbon did not appear to form at any appreciable rate on the copper coupons at the conditions shown in Table 14 below. No water was collected from the gases during the test.
Twelve coupons were cut from a sheet of brass and were washed in ethanol to remove contaminants and oxidation. The coupons were placed in quartz boats in a quartz tube as described above. A reaction gas containing about 45% H2 and 45% CO and 10% Ar was introduced into the quartz tube at about 4.0 MPa. The gases flowed over the coupons for about 4 hours at 1200 sccm. Solid carbon did not appear to form at any appreciable rate on the brass coupons at the conditions shown in Table 15 below. No water was collected from the gases during the test.
Three coupons were cut from a sheet of molybdenum metal and were washed in ethanol to remove contaminants and oxidation. The coupons were placed in quartz boats in a quartz tube as described above. A reaction gas containing about 45% H2 and 45% CO and 10% Ar was introduced into the quartz tube at about 4.0 MPa. The gases flowed over the coupons for about 4 hours at 2000 sccm. Solid carbon formed on each coupon at the rates shown in Table 16 below. Some methane and carbon dioxide formed in the quartz tube. After the test, solid carbon was physically removed from the coupons and measured, as shown in Table 16. Samples of the solid carbon were imaged using SEM, as shown in
Twelve coupons were cut from a sheet of cold-rolled steel (i.e., mild steel) and were washed in hydrochloric acid to remove contaminants and oxidation. The coupons were placed in quartz boats in a quartz tube as described above. A reaction gas containing about 45% H2 and 45% CO and 10% Ar was introduced into the quartz tube at about 4.0 MPa. The gases flowed over the coupons for about 4 hours at 1200 sccm. Solid carbon formed on each coupon at the rates shown in Table 17 below. Methane, carbon dioxide, and water were also formed in the quartz tube. After the test, solid carbon was physically removed from the coupons and tested for BET surface area, as shown in Table 17. Samples of the solid carbon were imaged using SEM, as shown in
Three pieces of wire, each about 2.5 cm to about 3.0 cm long, were cut from a roll of about 2.3 mm diameter molybdenum wire and were washed in ethanol to remove contaminants and oxidation. The wires were placed in quartz boats in a quartz tube as described above. A reaction gas containing about 50% H2 and 50% CO was introduced into the quartz tube at about 4.0 MPa. The gases flowed over the wires for about 4 hours at 2000 sccm. Solid carbon formed on each wire at the rates shown in Table 18 below. Methane, carbon dioxide, and water were also formed in the quartz tube. After the test, solid carbon was physically removed from the coupons and measured, as shown in Table 18. Samples of the solid carbon were imaged using SEM, as shown in
Twelve coupons were cut from a sheet of galvanized mild steel (i.e., mild steel treated with zinc oxide) that has been heat-treated (as available from Hercules Industries, of Denver, Colo., under the trade name PAINTLOCK) and were washed in ethanol to remove contaminants and oxidation. The coupons were placed in quartz boats in a quartz tube as described above. A reaction gas containing about 45% H2 and 45% CO and 10% Ar was introduced into the quartz tube at about 4.0 MPa. The gases flowed over the coupons for about 4 hours at 1200 sccm. Solid carbon formed on each coupon at the rates shown in Table 19 below. Methane, carbon dioxide, and water were also formed in the quartz tube. After the test, solid carbon was physically removed from the coupons and tested for BET surface area, as shown in Table 19. Samples of the solid carbon were imaged using SEM, as shown in
Twelve coupons were cut from a sheet of 316L stainless steel (i.e., an alloy having 16%-18.5% Cr, 10%-14% Ni, 2%-3% Mo, up to about 2% Mn, up to about 1% Si, up to about 0.045% P, up to about 0.03% S, up to about 0.03% C, with the balance Fe) and were washed in ethanol to remove contaminants and oxidation. The coupons were placed in quartz boats in a quartz tube as described above. A reaction gas containing about 45% H2 and 45% CO and 10% Ar was introduced into the quartz tube at about 4.0 MPa. The gases flowed over the coupons for about 4 hours at 1200 sccm. Solid carbon formed on each coupon at the rates shown in Table 20 below. Methane, carbon dioxide, and water were also formed in the quartz tube. After the test, solid carbon was physically removed from the coupons and tested for BET surface area, as shown in Table 20. Samples of the solid carbon were imaged using SEM, as shown in
Twelve coupons were cut from a sheet of 410 stainless steel (i.e., an alloy having 11.5%-13.5% Cr, at least 0.75% Ni, up to about 1% Mn, up to about 1% Si, up to about 0.04% P, up to about 0.03% S, up to about 0.015% C, with the balance Fe) and were washed in ethanol to remove contaminants and oxidation. The coupons were placed in quartz boats in a quartz tube as described above. A reaction gas containing about 45% H2 and 45% CO and 10% Ar was introduced into the quartz tube at about 4.0 MPa. The gases flowed over the coupons for about 4 hours at 1200 sccm. Solid carbon formed on each coupon at the rates shown in Table 21 below. Methane, carbon dioxide, and water were also formed in the quartz tube. After the test, solid carbon was physically removed from the coupons and tested for BET surface area, as shown in Table 21. Samples of the solid carbon were imaged using SEM, as shown in
Twelve samples of metal powder, comprising 92%-98% cast iron, were placed in quartz boats in a quartz tube as described above. A reaction gas containing about 45% H2 and 45% CO and 10% Ar was introduced into the quartz tube at about 4.0 MPa. The gases flowed over the metal powder for about 4 hours at 1200 sccm. Solid carbon formed on the metal powder at the rates shown in Table 22 below. Methane, carbon dioxide, and water were also formed in the quartz tube. After the test, solid carbon was tested for BET surface area, as shown in Table 22. Samples of the solid carbon were imaged using SEM, as shown in
Twelve coupons were cut from a sheet of 13-8H stainless steel (i.e., an alloy having 12.25%-13.5% Cr, 7.5%-8.5% Ni, 2.0%-2.5% Mo, 0.90%-1.35% Al, up to about 0.1% Mn, up to about 0.1% Si, up to about 0.01% P, up to about 0.05% C, up to about 0.01% N, and up to about 0.008% S with the balance Fe) and were washed in ethanol to remove contaminants and oxidation. The coupons were placed in quartz boats in a quartz tube as described above. A reaction gas containing about 45% H2 and 45% CO and 10% Ar was introduced into the quartz tube at about 4.0 MPa. The gases flowed over the coupons for about 4 hours at 1200 sccm. Solid carbon formed on each coupon at the rates shown in Table 23 below. Methane, carbon dioxide, and water were also formed in the quartz tube. After the test, samples of the solid carbon were imaged using SEM, as shown in
Twelve coupons were cut from a sheet of grade O1 tool steel (i.e., an alloy having about 0.90% C, 1.0%-1.4% Mn, about 0.50% Cr, about 0.50% Ni, and about 0.50% W, with the balance Fe) and were washed in ethanol to remove contaminants and oxidation. The coupons were placed in quartz boats in a quartz tube as described above. A reaction gas containing about 45% H2 and 45% CO and 10% Ar was introduced into the quartz tube at about 4.0 MPa. The gases flowed over the coupons for about 4 hours at 1200 sccm. Solid carbon formed on each coupon at the rates shown in Table 24 below. Methane, carbon dioxide, and water were also formed in the quartz tube. After the test, samples of the solid carbon were imaged using SEM, as shown in
Twelve coupons were cut from a sheet of 4140 steel (i.e., an alloy having about 0.42% C, about 1.0% Mn, about 1.0% Cr, about 0.30% Si, and about 0.20% Mo, with the balance Fe) and were washed in ethanol to remove contaminants and oxidation. The coupons were placed in quartz boats in a quartz tube as described above. A reaction gas containing about 45% H2 and 45% CO and 10% Ar was introduced into the quartz tube at about 4.0 MPa. The gases flowed over the coupons for about 4 hours at 1200 sccm. Solid carbon formed on each coupon at the rates shown in Table 25 below. Methane, carbon dioxide, and water were also formed in the quartz tube. About 10.5 grams of water were collected from the gases during the test.
Twelve coupons were cut from a sheet of M42 high speed steel (i.e., an alloy having about 1.1% C, about 9.5% Mo, about 3.8% Cr, about 1.5% W, about 1.2% V, and about 8.0% Co, with the balance Fe) and were washed in ethanol to remove contaminants and oxidation. The coupons were placed in quartz boats in a quartz tube as described above. A reaction gas containing about 45% H2 and 45% CO and 10% Ar was introduced into the quartz tube at about 4.0 MPa. The gases flowed over the coupons for about 4 hours at 1200 sccm. Solid carbon formed on each coupon at the rates shown in Table 26 below. Methane, carbon dioxide, and water were also formed in the quartz tube. About 17.8 grams of water were collected from the gases during the test.
Twelve coupons were cut from a sheet of D2 tool steel (i.e., an alloy having about 1.5% C, 11.0%-13.0% Cr, about 0.45% Mn, about 0.03% P, about 1.0% V, about 0.9% Mo, and about 0.3% S, with the balance Fe) and were washed in ethanol to remove contaminants and oxidation. The coupons were placed in quartz boats in a quartz tube as described above. A reaction gas containing about 45% H2 and 45% CO and 10% Ar was introduced into the quartz tube at about 4.0 MPa. The gases flowed over the coupons for about 4 hours at 1200 sccm. Solid carbon formed on each coupon at the rates shown in Table 27 below. Methane, carbon dioxide, and water were also formed in the quartz tube. About 14.2 grams of water were collected from the gases during the test.
Twelve coupons were cut from a sheet of 1045 steel (i.e., an alloy having 0.42%-0.5% C, 0.6%-0.9% Mn, up to about 0.04% P, and up to about 0.5% S, with the balance Fe) and were washed in ethanol to remove contaminants and oxidation. The coupons were placed in quartz boats in a quartz tube as described above. A reaction gas containing about 45% H2 and 45% CO and 10% Ar was introduced into the quartz tube at about 4.0 MPa. The gases flowed over the coupons for about 4 hours at 1200 sccm. Solid carbon formed on each coupon at the rates shown in Table 28 below. Methane, carbon dioxide, and water were also formed in the quartz tube. About 13.4 grams of water were collected from the gases during the test.
Ten samples, each approximately 2 cm long, were cut from a cobalt rod having a diameter of about 2 mm, and were washed in ethanol to remove contaminants and oxidation. The samples were placed in quartz boats in a quartz tube as described above. A reaction gas containing about 45% H2 and 45% CO and 10% Ar was introduced into the quartz tube at about 4.0 MPa. The gases flowed over the cobalt samples for about 4 hours at 1200 sccm. Solid carbon formed on each sample at the rates shown in Table 29 below. Methane, carbon dioxide, and water were also formed in the quartz tube. About 1.93 grams of water were collected from the gases during the test.
Twelve samples, each approximately 2.3-2.7 cm long, were cut from a titanium rod having a diameter of about 1.65 mm, and were washed in ethanol to remove contaminants and oxidation. The samples were placed in quartz boats in a quartz tube as described above. A reaction gas containing about 45% H2 and 45% CO and 10% Ar was introduced into the quartz tube at about 4.0 MPa. The gases flowed over the cobalt samples for about 4 hours at 1200 sccm. Solid carbon formed on each sample at the rates shown in Table 30 below. Methane, carbon dioxide, and water were also formed in the quartz tube. No water was collected from the gases during the test.
The experiment of Example 1 is repeated with a nickel-containing catalyst. The reactor temperature is maintained in excess of 680° C. The pressure of the reactor is controlled and may range from atmospheric pressure to pressures in excess of 6.2 MPa (900 psig). The carbon dioxide is thus reduced in the presence of a nickel-containing catalyst. The size and morphology of the solid carbon product is controlled by the grain size of the nickel-containing catalyst.
The experiment of Example 2 is repeated with a mixture of nickel and chromium as the catalyst. The carbon dioxide is reduced in the presence of the catalyst. The size and morphology of the resulting solid carbon product is controlled by the grain size of the nickel and chromium containing catalyst.
The experiment of Example 3 is repeated with methane used as the reducing agent in the place of hydrogen. Solid carbon nanotubes are formed by reducing carbon oxides with methane gas. The methane gas may also be combusted to provide the carbon oxide to be reduced. Carbon oxides created by the incomplete combustion of methane are reduced in the presence of methane to create solid CNTs. The combustion of methane forms carbon dioxide and water:
CH4+2O2CO2+2H2O (Equation 7).
The carbon dioxide produced in Equation 7 is reduced by methane in the presence of a catalyst as shown in Equation 4. The size and morphology of the resulting solid carbon product is controlled by the grain size of the catalyst.
The experiment of Example 4 is repeated in a fluidized-bed reactor. The reactor is configured such that the solid carbon product is elutriated from the reactor due to the drag forces on the particles. The size and shape of the catalyst particles are selected to have a relatively large contact surface area between the catalyst and the reactant gases.
Although the foregoing description contains specific details, these are not to be construed as limiting the scope of the present invention, but merely as providing certain embodiments. Similarly, other embodiments of the invention may be devised that do not depart from the scope of the present invention. For example, features described herein with reference to one embodiment also may be provided in others of the embodiments described herein. The scope of the invention is, therefore, indicated and limited only by the appended claims and their legal equivalents, rather than by the foregoing description. All additions, deletions, and modifications to the invention, as disclosed herein, which fall within the meaning and scope of the claims, are encompassed by the present invention.
This application claims the benefit of the filing date of U.S. Provisional Patent Application Ser. No. 61/624,702, filed Apr. 16, 2012, for “Methods and Structures for Producing Solid Carbon Utilizing Non-Ferrous Catalysts,” the disclosure of which is hereby incorporated herein in its entirety by this reference.
| Filing Document | Filing Date | Country | Kind |
|---|---|---|---|
| PCT/US2013/000072 | 3/15/2013 | WO | 00 |
| Publishing Document | Publishing Date | Country | Kind |
|---|---|---|---|
| WO2013/158156 | 10/24/2013 | WO | A |
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| Number | Date | Country | |
|---|---|---|---|
| 20150086468 A1 | Mar 2015 | US |
| Number | Date | Country | |
|---|---|---|---|
| 61624702 | Apr 2012 | US |
